CN103524300B - Method for jointly producing methyl alcohol by using water gas and coke oven gas - Google Patents
Method for jointly producing methyl alcohol by using water gas and coke oven gas Download PDFInfo
- Publication number
- CN103524300B CN103524300B CN201310491497.7A CN201310491497A CN103524300B CN 103524300 B CN103524300 B CN 103524300B CN 201310491497 A CN201310491497 A CN 201310491497A CN 103524300 B CN103524300 B CN 103524300B
- Authority
- CN
- China
- Prior art keywords
- gas
- mixed gas
- methyl alcohol
- oven
- water
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/1516—Multisteps
- C07C29/1518—Multisteps one step being the formation of initial mixture of carbon oxides and hydrogen for synthesis
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23K—FEEDING FUEL TO COMBUSTION APPARATUS
- F23K5/00—Feeding or distributing other fuel to combustion apparatus
- F23K5/002—Gaseous fuel
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Industrial Gases (AREA)
Abstract
The invention provides a method for jointly producing methyl alcohol by using water gas and coke oven gas, and relates to a methyl alcohol production method. The method is used for solving the technical problem that no appropriate fuel gas is supplied for replacing pure gas to serve as heating fuel of a preheating furnace in a conventional process of using the coke oven gas for producing the methyl alcohol. The method comprises the following steps: feeding the water gas and the coke oven gas into a gas holder, feeding into a wet desulphurization tower for desulphurization, then carrying out continuous fine desulphurization through a preliminary desulphurization tower, a ferrum-molybdenum converter, a cobalt-molybdenum converter and a ferric oxide desulfurizer, afterwards, dividing the mixed gas subjected to the fine desulfurization into two parts, feeding the first part of mixed gas into the preheating gas so as to heat the first part of mixed gas, and then enabling the first part of mixed gas to enter a converting furnace so as to convert the first part of mixed gas, thus obtaining synthesis gas; guiding the second part of the mixed gas into a burner of the preheating furnace, igniting the second part of the mixed gas so as to serve as the fuel of the preheating furnace; and feeding the synthesis gas into a synthesis tower, cooling and separating the synthesized methyl alcohol, then rectifying a liquid phase so as to obtain a methyl alcohol product, feeding the separated gas phase into a coal tar hydrogenation pressure swing adsorption device, and recycling hydrogen. The method is used for jointly producing the methyl alcohol by using the water gas and the coke oven gas.
Description
Technical field
The present invention relates to the production method of methyl alcohol.
Background technology
The process of employing coke-oven gas methanol is: coke-oven gas passes in gas holder, then sends into the thick desulfurization of wet desulfuration tower through blower fan; And then through compressor compression after, carry out fine de-sulfur through pre-thionizer, cobalt molybdenum convertor, the process of ferric oxide devulcanizer, then after preheating oven preheating, converter partial oxidation, again pressurization, enter synthetic tower synthesizing methanol, obtain thick first after refrigerated separation, liquid phase is through rectification process, obtain methanol product, 85% of gas phase is back to synthesis stage and carries out recycle, and 15% of remainder is off-gas, heating medium as preheating oven passes into preheating oven combustion heat release, and its process flow diagram as shown in Figure 1.In the process of this coke-oven gas methanol, off-gas produces heat as the fuel of preheating oven, due in off-gas hydrogeneous more than 80%, and hydrogen is the important source material of coal tar hydrogenating link, off-gas all must supply the full production of coal tar hydrogenating unit guarantee coal tar hydrogenating.Current off-gas should supply coal tar hydrogenating unit, and again as the fuel of preheating oven, both are difficult to take into account the difficult point becoming and perplex existing coke-oven gas methanol.
Summary of the invention
The present invention does not have suitable fuel gas to substitute the technical problem of off-gas as the heating fuel of preheating oven in the process that will solve existing coke-oven gas methanol, and provides a kind of method of water-gas and coke-oven gas co-production methyl alcohol.
The method of a kind of water-gas of the present invention and coke-oven gas co-production methyl alcohol, specifically carry out according to the following steps:
One, pass in gas holder by the water-gas of blue-gas generator output, mix, obtain mixed gas with the coke(oven)gas passing into gas holder in gas holder, wherein in mixed gas, the volume percent of water-gas is 15% ~ 30%;
Two, the mixed gas in gas holder being forced into gauge pressure through blower fan is 20 ~ 30KPa, enters wet desulfuration tower, contacts, by the hydrogen sulfide stripping in mixed gas to below 20mg/L with doctor solution lean solution is reverse;
Three, the mixed gas through step 2 process being pressurized to gauge pressure through compressor is 2.2 ~ 2.8MPa, through the continuous fine desulfurization of pre-thionizer, iron molybdenum convertor, cobalt molybdenum convertor, ferric oxide devulcanizer, is taken off by the total sulfur content of mixed gas to being less than 0.1ppm;
Four, the mixed gas through step 3 process is divided into two portions, wherein first part's mixed gas passes into preheating oven; Second section mixed gas is incorporated in the burner of preheating oven, and ignition is as the fuel of preheating oven; Wherein the volume ratio of first part's mixed gas and second section mixed gas is 10 ~ 15:1, and in preheating oven, mixed gas is warming up to 600 ~ 620 DEG C, then enters converter, the methane conversion in mixed gas is become carbon monoxide and hydrogen, obtains synthetic gas;
Five, the synthetic gas that step 4 obtains is 3.2 ~ 3.8MPa through synthesizing compressor pressurizes to gauge pressure, send into synthetic tower, synthesizing methanol under the effect of synthesizing methanol catalyst, synthetic tower Outlet Gas Temperature controls at 280 ~ 300 DEG C, liquid phase after gas cooling is separated is crude carbinol, crude carbinol, again after rectifying, obtains methanol product; 85% of the volume of the gas phase after gas cooling is separated is back to synthetic compressor circulation, and 15% of the volume of gas phase delivers to coal tar hydrogenating pressure-swing absorption apparatus, reclaims and obtains hydrogen.
The present invention changes conventional to be rich in the off-gas of 80% hydrogen as the way of preheating oven as fuel, but the water-gas of cheapness is applied in methanol process, get the gas mixture of partial water gas and coke(oven)gas as preheating oven fuel, and the off-gas of methyl alcohol synthetic reactor is used for extract hydrogen, the ratio of the gas mixture as fuel gas and the mixed gas as synthetic gas is used for by choose reasonable, the ability discharged as fuel gas part is exactly met by the requirement of heated air, make economic benefit improve 15% ~ 40%, receive good effect.Method of the present invention has saved the expensive enriched gas source of guarantor, have received good effect, and the burner in preheating oven does not need to do any change, just can directly adopt coke-oven gas and water-gas propellant combination for preheating oven.
The present invention adopts water-gas and coke(oven)gas mixed gas as the raw materials for production of methyl alcohol, both ensure that the quality of production and the purity of methyl alcohol, again can effective production control cost.Utilize water-gas and coke(oven)gas mixed gas to heat up to preheating oven simultaneously, ensure to provide preheating oven react needed for enough calorific values, can avoid again being used alone coke(oven)gas or water-gas calorific value is too high or too low, the problem that preheating oven temperature is not up to standard.
Accompanying drawing explanation
Fig. 1 is the process flow diagram of prior art;
Fig. 2 is the process flow diagram of embodiment one.
Embodiment
Embodiment one: a kind of water-gas of present embodiment and the method for coke-oven gas co-production methyl alcohol, specifically carry out according to the following steps:
One, pass in gas holder by the water-gas of blue-gas generator output, mix, obtain mixed gas with the coke(oven)gas passing into gas holder in gas holder, wherein in mixed gas, the volume percent of water-gas is 15% ~ 30%;
Two, the mixed gas in gas holder being forced into gauge pressure through blower fan is 20 ~ 30KPa, enters wet desulfuration tower, contacts, by the hydrogen sulfide stripping in mixed gas to below 20mg/L with doctor solution lean solution is reverse;
Three, the mixed gas through step 2 process being pressurized to gauge pressure through compressor is 2.2 ~ 2.8MPa, through the continuous fine desulfurization of pre-thionizer, iron molybdenum convertor, cobalt molybdenum convertor, ferric oxide devulcanizer, is taken off by the total sulfur content of mixed gas to being less than 0.1ppm;
Four, the mixed gas through step 3 process is divided into two portions, wherein first part's mixed gas passes into preheating oven; Second section mixed gas is incorporated in the burner of preheating oven, and ignition is as the fuel of preheating oven; Wherein the volume ratio of first part's mixed gas and second section mixed gas is 10 ~ 15:1, and in preheating oven, mixed gas is warming up to 600 ~ 620 DEG C, then enters converter, the methane conversion in mixed gas is become carbon monoxide and hydrogen, obtains synthetic gas;
Five, the synthetic gas that step 4 obtains is 3.2 ~ 3.8MPa through synthesizing compressor pressurizes to gauge pressure, send into synthetic tower, synthesizing methanol under the effect of synthesizing methanol catalyst, synthetic tower Outlet Gas Temperature controls at 280 ~ 300 DEG C, liquid phase after gas cooling is separated is crude carbinol, crude carbinol, again after rectifying, obtains methanol product; 85% of the volume of the gas phase after gas cooling is separated is back to synthetic compressor circulation, and 15% of the volume of gas phase delivers to coal tar hydrogenating pressure-swing absorption apparatus, reclaims and obtains hydrogen.
Embodiment two: present embodiment and embodiment one consist of unlike the volume percent of water-gas in step one: carbon monoxide is 40% ~ 50%, hydrogen is 32 ~ 38%, carbonic acid gas 16 ~ 20%, and all the other are impurity.Other are identical with embodiment one.
Embodiment three: present embodiment and embodiment one or two are 25 ~ 28KPa unlike the mixed gas in gas holder being forced into gauge pressure through blower fan in step 2.Other are identical with embodiment one.
Embodiment four: one of present embodiment and embodiment one to three are soda ash unlike the doctor solution in step 2.Other are identical with one of embodiment one to three.
Embodiment five: it is 2.5 ~ 2.7MPa that one of present embodiment and embodiment one to four are pressurized to gauge pressure unlike mixed gas in step 3 through compressor.Other are identical with one of embodiment one to four.
Embodiment six: one of present embodiment and embodiment one to five take off to 0.05ppm unlike the total sulfur content of mixed gas in step 3.Other are identical with one of embodiment one to five.
Embodiment seven: one of present embodiment and embodiment one to six are 12 ~ 13:1 unlike the volume ratio of first part's mixed gas and second section mixed gas in step 4.Other are identical with one of embodiment one to six.
Embodiment eight: one of present embodiment and embodiment one to seven pass in preheating oven unlike first part's mixed gas in step 4 and be warming up to 610 ~ 615 DEG C.Other are identical with one of embodiment one to seven.
Embodiment nine: it is 3.4 ~ 3.6MPa that one of present embodiment and embodiment one to eight are pressurized to gauge pressure unlike synthetic gas in step 5.Other are identical with one of embodiment one to eight.
Embodiment ten: one of present embodiment and embodiment one to nine control at 285 ~ 295 DEG C unlike synthetic tower temperature out in step 5.Other are identical with one of embodiment one to nine.
Embodiment 11: one of present embodiment and embodiment one to ten are copper-based catalysts unlike synthetic tower catalyst in step 5.Other are identical with one of embodiment one to ten.
Embodiment 12: one of present embodiment and embodiment one to ten one unlike synthetic gas in step 5 composition by volume per-cent be the impurity of the hydrogen of 60 ~ 65%, the carbon monoxide of 20 ~ 30% and surplus.Other are identical with one of embodiment one to ten one.
Impurity described in present embodiment is methane and nitrogen.
With following verification experimental verification beneficial effect of the present invention:
Test 1: a kind of water-gas of this test 1 and the method for coke-oven gas co-production methyl alcohol, specifically carry out according to the following steps:
One, pass in gas holder by the water-gas of blue-gas generator output, mix, obtain mixed gas with the coke(oven)gas passing into gas holder in gas holder, wherein in mixed gas, the volume percent of water-gas is 25%;
Wherein the volume percent of water-gas consists of: carbon monoxide is 45%, hydrogen is 35%, and carbonic acid gas is 18%, and all the other are impurity;
Two, the mixed gas in gas holder being forced into gauge pressure through blower fan is 20KPa, enters wet desulfuration tower, contacts, by the hydrogen sulfide stripping in mixed gas to 9mg/L with doctor solution soda ash lean solution is reverse;
Three, the mixed gas through step 2 process being pressurized to gauge pressure through compressor is 2.5MPa, through the continuous fine desulfurization of pre-thionizer, iron molybdenum convertor, cobalt molybdenum convertor, ferric oxide devulcanizer, takes off to 0.08ppm by the total sulfur content of mixed gas;
Four, the mixed gas through step 3 process is divided into two portions, wherein first part's mixed gas passes into preheating oven; Second section mixed gas is incorporated in the burner of preheating oven, and ignition is as the fuel of preheating oven; Wherein the volume ratio of first part's mixed gas and second section mixed gas is 10:1, in preheating oven, mixed gas is warming up to 620 DEG C, then converter is entered, methane conversion in mixed gas is become carbon monoxide and hydrogen, obtain synthetic gas, in synthetic gas, the volume percent of hydrogen is 60%, and carbonic oxide is 30%, nitrogen is 5%, and methane is 5%;
Five, the synthetic gas that step 4 obtains is pressurized to 3.5MPa, sends into synthetic tower, synthesizing methanol under the effect of catalyst copper-based catalysts, synthetic tower Outlet Gas Temperature controls at 290 DEG C, liquid phase after gas cooling is separated is crude carbinol, and crude carbinol, again after rectifying, obtains methanol product; 85% of the volume of the gas phase after gas cooling is separated is back to synthetic compressor circulation, and 15% of the volume of gas phase delivers to coal tar hydrogenating pressure-swing absorption apparatus, reclaims and obtains hydrogen.
This test 1 changes conventional to be rich in the off-gas of 80% hydrogen as the way of preheating oven as fuel, but the water-gas of cheapness is applied in methanol process, get the gas mixture of partial water gas and coke(oven)gas as preheating oven fuel, and the off-gas of methyl alcohol synthetic reactor is used for extract hydrogen, the ratio of the gas mixture as fuel gas and the mixed gas as synthetic gas is used for by choose reasonable, the ability discharged as fuel gas part is exactly met by the requirement of heated air, economic benefit is made to improve 30%, if calculate by this, 1 year can fecund go out about 6,000 ten thousand economic benefit, considerable, receive good effect.The method of this test has saved the expensive enriched gas source of guarantor, have received good effect, and the burner in preheating oven does not need to do any change, just can directly adopt coke-oven gas and water-gas propellant combination for preheating oven, to original processing unit basis being changed conveniently.
Claims (9)
1. a method for water-gas and coke-oven gas co-production methyl alcohol, is characterized in that the method is specifically carried out according to the following steps:
One, pass in gas holder by the water-gas of blue-gas generator output, mix, obtain mixed gas with the coke(oven)gas passing into gas holder in gas holder, wherein in mixed gas, the volume percent of water-gas is 15% ~ 30%;
Two, the mixed gas in gas holder being forced into gauge pressure through blower fan is 20 ~ 30KPa, enters wet desulfuration tower, contacts, by the hydrogen sulfide stripping in mixed gas to below 20mg/L with doctor solution lean solution is reverse;
Three, the mixed gas through step 2 process being pressurized to gauge pressure through compressor is 2.2 ~ 2.8MPa, through the continuous fine desulfurization of pre-thionizer, iron molybdenum convertor, cobalt molybdenum convertor and ferric oxide devulcanizer, is taken off by the total sulfur content of mixed gas to being less than 0.1ppm;
Four, the mixed gas through step 3 process is divided into two portions, wherein first part's mixed gas passes into preheating oven; Second section mixed gas is incorporated in the burner of preheating oven, and ignition is as the fuel of preheating oven; Wherein the volume ratio of first part's mixed gas and second section mixed gas is 10 ~ 15:1, and in preheating oven, mixed gas is warming up to 600 ~ 620 DEG C, then enters converter, the methane conversion in mixed gas is become carbon monoxide and hydrogen, obtains synthetic gas;
Five, the synthetic gas that step 4 obtains is 3.2 ~ 3.8MPa through synthesizing compressor pressurizes to gauge pressure, send into synthetic tower, synthesizing methanol under the effect of synthesizing methanol catalyst, synthetic tower Outlet Gas Temperature controls at 280 ~ 300 DEG C, liquid phase after gas cooling is separated is crude carbinol, crude carbinol, again after rectifying, obtains methanol product; 85% of the volume of the gas phase after gas cooling is separated is back to synthetic compressor circulation, and 15% of the volume of gas phase delivers to coal tar hydrogenating pressure-swing absorption apparatus, reclaims and obtains hydrogen.
2. the method for a kind of water-gas according to claim 1 and coke-oven gas co-production methyl alcohol, it is characterized in that in step one, the volume percent of water-gas consists of: carbon monoxide is 40% ~ 50%, hydrogen is 32% ~ 38%, carbonic acid gas 16% ~ 20%, all the other are impurity.
3. the method for a kind of water-gas according to claim 1 and 2 and coke-oven gas co-production methyl alcohol, is characterized in that in step 2, the mixed gas in gas holder being forced into gauge pressure through blower fan is 25 ~ 28KPa.
4. the method for a kind of water-gas according to claim 1 and 2 and coke-oven gas co-production methyl alcohol, is characterized in that the doctor solution in step 2 is soda ash.
5. the method for a kind of water-gas according to claim 1 and 2 and coke-oven gas co-production methyl alcohol, it is characterized in that in step 3 that mixed gas is pressurized to gauge pressure through compressor is 2.5 ~ 2.7MPa.
6. the method for a kind of water-gas according to claim 1 and 2 and coke-oven gas co-production methyl alcohol, is characterized in that in step 3, the total sulfur content of mixed gas takes off to 0.05ppm.
7. the method for a kind of water-gas according to claim 1 and 2 and coke-oven gas co-production methyl alcohol, is characterized in that the volume ratio of first part's mixed gas and second section mixed gas in step 4 is 12 ~ 13:1.
8. the method for a kind of water-gas according to claim 1 and 2 and coke-oven gas co-production methyl alcohol, to is characterized in that in step 4 that first part's mixed gas passes in preheating oven and is warming up to 610 ~ 615 DEG C.
9. the method for a kind of water-gas according to claim 1 and 2 and coke-oven gas co-production methyl alcohol, is characterized in that in step 5, synthetic tower catalyst is copper-based catalysts.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310491497.7A CN103524300B (en) | 2013-10-18 | 2013-10-18 | Method for jointly producing methyl alcohol by using water gas and coke oven gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310491497.7A CN103524300B (en) | 2013-10-18 | 2013-10-18 | Method for jointly producing methyl alcohol by using water gas and coke oven gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103524300A CN103524300A (en) | 2014-01-22 |
| CN103524300B true CN103524300B (en) | 2015-04-08 |
Family
ID=49926711
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310491497.7A Active CN103524300B (en) | 2013-10-18 | 2013-10-18 | Method for jointly producing methyl alcohol by using water gas and coke oven gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103524300B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104130104A (en) * | 2014-07-03 | 2014-11-05 | 兖矿集团有限公司煤化分公司 | Method for making gas, supplementing carbon and increasing methanol yield by chopped coke with 7-24mm |
| CN104086368B (en) * | 2014-07-23 | 2015-07-08 | 北京众联盛化工工程有限公司 | Method for regulating H/C ratio in preparation of methanol by use of coke oven gas |
| CN112142559A (en) * | 2020-09-22 | 2020-12-29 | 吕永华 | Waste heat recovery device for methanol production |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101434879A (en) * | 2008-12-15 | 2009-05-20 | 四川天一科技股份有限公司 | Method for preparing methyl alcohol synthesis gas and compressed natural gas from coke oven gas and coal |
| CN101538483A (en) * | 2009-04-03 | 2009-09-23 | 中国科学院山西煤炭化学研究所 | Poly-generation technique for using coal gas and coke oven gas as raw materials |
| CN101597527A (en) * | 2009-07-07 | 2009-12-09 | 山西科灵环境工程设计技术有限公司 | A kind of method of utilizing coke(oven)gas to produce synthetic natural gas |
| CN101704712A (en) * | 2009-10-29 | 2010-05-12 | 山西焦化股份有限公司 | Technological method for preparing methanol by combining coke oven gas with water gas |
-
2013
- 2013-10-18 CN CN201310491497.7A patent/CN103524300B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101434879A (en) * | 2008-12-15 | 2009-05-20 | 四川天一科技股份有限公司 | Method for preparing methyl alcohol synthesis gas and compressed natural gas from coke oven gas and coal |
| CN101538483A (en) * | 2009-04-03 | 2009-09-23 | 中国科学院山西煤炭化学研究所 | Poly-generation technique for using coal gas and coke oven gas as raw materials |
| CN101597527A (en) * | 2009-07-07 | 2009-12-09 | 山西科灵环境工程设计技术有限公司 | A kind of method of utilizing coke(oven)gas to produce synthetic natural gas |
| CN101704712A (en) * | 2009-10-29 | 2010-05-12 | 山西焦化股份有限公司 | Technological method for preparing methanol by combining coke oven gas with water gas |
Non-Patent Citations (1)
| Title |
|---|
| "水煤气、焦炉煤气联产甲醇工艺的探索与实践";李毓良 等;《山东化工》;20111231;第40卷(第4期);70-71 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103524300A (en) | 2014-01-22 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110770162B (en) | Method for producing ammonia synthesis gas | |
| CN101368010B (en) | Method for producing semi-reinforcing hydrocarbon black, methanol, liquid ammonia with coke oven gas | |
| KR20210151778A (en) | chemical synthesis plant | |
| CN101508922B (en) | Methanation reaction process using oven gas to prepare substitute natural gas | |
| CN103351894B (en) | Natural gas synthesizing technology adopting coke oven gas and coal gasifier gas | |
| CN1974732A (en) | Process of preparing synthesized gas with gasified gas and pyrolyzed gas | |
| CN102585951A (en) | Novel process for co-production of liquefied synthesis gas, pure hydrogen and methanol from coke-oven gas | |
| CN103303863A (en) | Method for producing ammonia synthesis gas from coke-oven gas | |
| CN104709876A (en) | Process method for preparing synthesis gas by using zero carbon or negative carbon emission system | |
| CN105883851B (en) | A kind of Novel gasification and pyrolysis coupling coal gas multi-production process | |
| KR20210151776A (en) | chemical synthesis plant | |
| CN103694074A (en) | System and process for preparing olefin by taking coal and coke-oven gas as raw materials | |
| CN103524300B (en) | Method for jointly producing methyl alcohol by using water gas and coke oven gas | |
| JP5763054B2 (en) | Method for simultaneously producing iron and crude synthesis gas containing CO and H 2 | |
| CN104830391A (en) | Methanation device and process for synthesizing high-quality natural gas produced by coal | |
| CN102876411A (en) | Method and device for producing synthetic natural gas | |
| CN110862839A (en) | System and method for co-production of methanol from coal-based natural gas | |
| CN102676251B (en) | Process for preparing methane by utilizing coke oven gas | |
| CN102746870B (en) | FT synthesis technology | |
| CN101302139A (en) | Method for preparing methanol using coal bed gas | |
| CN104987892A (en) | Chemical-power polygeneration system adopting chemical unreacted gas to moderately circulate based on graded gasification | |
| CN101818087A (en) | Novel process for making synthetic natural gas by using coke-oven gas | |
| CN105861070A (en) | Technology for synthesizing methanol dimethyl ether through biomass gasification | |
| CN106748655A (en) | It is a kind of efficiently to reduce integrated iron and steel works CO2The method of discharge | |
| CN103013598B (en) | Method and device for producing synthesized natural gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of invention: Method of co-production of methanol from water gas and coke oven gas Effective date of registration: 20230104 Granted publication date: 20150408 Pledgee: Qitaihe Rural Commercial Bank Co.,Ltd. Xinxing sub branch Pledgor: QITAIHE BAOTAILONG METHANOL Co.,Ltd. Registration number: Y2023230000004 |